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A kind of starting method of hydrogenation catalyst

A hydrogenation catalyst and catalyst technology are applied in the fields of hydrotreating process, petroleum industry, processing hydrocarbon oil, etc., to save manpower, stop consumption, and avoid the poisoning of vulcanizing agent to human body.

Active Publication Date: 2015-09-30
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0006] Aiming at the problems existing in the existing start-up technology, the present invention provides a method for start-up of a hydrogenation catalyst. In this method, hydrogen sulfide-enriched oil and back-extracted oil from liquefied gas desulfurization are combined step by step as the start-up process of the hydrogenation catalyst. The vulcanizing agent can completely avoid the problem of external pre-vulcanization and the consumption of vulcanizing agent during the start-up process, which not only saves energy, but also reduces the pollution of the vulcanizing agent to the environment

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  • A kind of starting method of hydrogenation catalyst

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Embodiment approach

[0030] Such as figure 1 As shown, an embodiment of the hydrogenation catalyst start-up method of the present invention is as follows:

[0031] The hydrogen sulfide enriched oil 1 passes through the raw material buffer tank 2 and the heating furnace 3, mixes with hydrogen gas 12, and then enters the hydrofining reactor 4 with an inlet temperature of 170°C, the hydrocracking reactor 5, and the reaction effluent 6 enters the high pressure Separator 8, the gas phase 9 obtained at the top is compressed by the circulating hydrogen compressor 10 and mixed with new hydrogen 11 to obtain hydrogen 12, the liquid phase 13 obtained at the bottom of the high-pressure separator 8 enters the low-pressure separator 14, and the separated gas phase 17 is exhausted Treatment, the liquid phase 18 can be used as a product after the fractionation 19 is removed from the device, and the liquid phase water 15 and 16 obtained at the bottom of the high-pressure separator 8 and the low-pressure separator...

Embodiment 1

[0037] After the hydrogen airtightness of the hydrocracking unit is qualified, the hydrogen partial pressure of the reaction system is adjusted to 12.0MPa, and the temperature is raised at 20°C / h. Naphtha is used as vulcanized oil, and naphtha is used in a one-pass process, and naphtha is added from the top of the reactor to the reactor for wetting. After the bed was wetted, the temperature at the reactor inlet was raised to 220°C at 10°C / h to keep the temperature constant.

[0038] When the hydrogen sulfide concentration at the outlet of the hydrocracking reactor reaches 0.13v%, it is considered that the hydrogen sulfide has penetrated the catalyst bed. Cut the naphtha rich in hydrogen sulfide out of this unit, and put it into the liquefied gas sweetening unit after the low fraction of the hydrogenation unit, use the back-extracted oil as the sulfurized oil, and use the hydrogenation reactor-high fraction-low fraction - Liquefied gas stripping - stripping oil circulation mod...

Embodiment 2

[0041] After the hydrogen airtightness of the hydrocracking unit is qualified, the hydrogen partial pressure of the reaction system is adjusted to 14.0MPa, and the temperature is raised at 20°C / h. Naphtha is used as vulcanized oil, and naphtha is used in a one-pass process, and naphtha is added from the top of the reactor to the reactor for wetting. After the bed was wetted, the temperature at the reactor inlet was raised to 235°C at 10°C / h to keep the temperature constant.

[0042] When the hydrogen sulfide concentration at the outlet of the hydrocracking reactor reaches 0.19v%, it is considered that the hydrogen sulfide has penetrated the catalyst bed. Cut the naphtha rich in hydrogen sulfide out of this unit, and put it into the liquefied gas sweetening unit after the low fraction of the hydrogenation unit, use the back-extracted oil as the sulfurized oil, and use the hydrogenation reactor-high fraction-low fraction - Liquefied gas stripping - stripping oil circulation mod...

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Abstract

The invention discloses a startup method of an oxidation state hydrogenation catalyst. The method consists of: in a catalyst vulcanization process, before hydrogen sulfide penetrates a catalyst bed, taking hydrogenated crude naphtha rich in hydrogen sulfide as vulcanization oil, and employing crude naphtha to pass through the process in one time; and when the hydrogen sulfide penetrates the catalyst bed, stopping injecting the crude naphtha, connecting a liquefied gas mercaptan removal device behind a hydrogenation unit low pressure separator in series, adopting reverse extract oil as vulcanization oil, and employing an operation mode of full cycle of the reverse extract oil until completion of catalyst vulcanization. The method disclosed in the invention respectively takes hydrogen sulfide-rich oil and liquefied gas desulfurization reverse extract oil as startup vulcanizing agents at different vulcanization stages, so that the startup vulcanizing agent consumption problem can be completely avoided. The method not only saves energy, but also reduces the pollution of the vulcanizing agents to the environment.

Description

technical field [0001] The invention relates to a hydrogenation catalyst start-up method, mainly through the use of hydrogen sulfide enriched oil and a combined liquefied gas desulfurization device to achieve the purpose of not using a sulfurizing agent, and is applicable to the principle start-up process of catalytic hydrogenation catalysts in various oxidation states . Background technique [0002] The hydrogenation catalysts currently produced in the domestic industry are basically oxidation-type. New catalysts or regenerated catalysts produced in industry contain active metal components (Mo, Ni, Co, W) in the oxidation state (MoO 3 , NiO, CoO, WO 3 ) exists in the form of The practice of basic research and industrial application shows that most of the active metal components of hydrogenation catalysts have higher hydrogenation activity and activity stability in their sulfide state. Before the hydrogenation catalyst is in contact with the hydrocarbon feedstock, a sulf...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G67/00
Inventor 潘德满王仲义石友良彭冲黄新露白振民孙士可
Owner CHINA PETROLEUM & CHEM CORP